|Publication number||US5817904 A|
|Application number||US 08/479,002|
|Publication date||Oct 6, 1998|
|Filing date||Jun 7, 1995|
|Priority date||Dec 11, 1992|
|Publication number||08479002, 479002, US 5817904 A, US 5817904A, US-A-5817904, US5817904 A, US5817904A|
|Inventors||Sebastian Vic, Miguel A. Pena, Pilar Terreros, Juan P. Gomez, Jose L. Garcia-Fierro, Juan M. Jimenez|
|Original Assignee||Repsol Petroleo S.A.|
|Export Citation||BiBTeX, EndNote, RefMan|
|Patent Citations (10), Referenced by (40), Classifications (16), Legal Events (5)|
|External Links: USPTO, USPTO Assignment, Espacenet|
This is a continuation of application Ser. No. 07/989,131, filed on Dec. 11, 1992, which was abandoned upon the filing hereof.
The invention relates to a catalytic method useful in the conversion of methane into higher hydrocarbons, particularly ethylene and ethane, via an oxidative coupling reaction of methane (OCM). The invention also refers to an improved catalyst composition for carrying out said method.
Natural gas, whose major component is methane, represents today the largest energy source. Its reserves are much larger than that of other fossil fuels, but are usually located in remote areas far enough from the market spots. Moreover, the methane molecule presents unfavourable critical constants which make it very difficult to be liquefied. Accordingly, the conversion of methane into easier liquefiable hydrocarbons, i.e. C2 + hydrocarbons, becomes imperative.
The discovery by Keller and Bhasin (J. Catal. 73,9,1982) that methane can be dimerised over redox type oxides was an improvement in this field. The disclosure of this work mentioned that methane can readily be converted over appropriate catalysts into C2 + hydrocarbons with a low yield and ranges of methane conversion between 9-48%. Detailed analysis of the results of the oxidative coupling led to the conclusion that this reaction is only selective for C2 + hydrocarbons when no oxygen is present in the gas phase, that is, the coupling is achieved by the lattice oxygen of the catalyst agent. Since lattice oxygen available from a redox system is limited for given reaction conditions, the reaction progress will also be limited. Furthermore, the cyclic operation implies large investment and significant time wasted for operation.
U.S. Pat. No. 4,443,644 discloses a process for the conversion of methane into higher hydrocarbons by contacting a methane-containing gas and solid particles comprising a reducible oxide of antimony at a temperature ranging from 500°-1000° C. to form higher hydrocarbon products, byproduct water and particles comprising a reduced oxide of antimony. The particles comprising a reduced oxide of antimony are removed and regenerated by contact with an oxygen-containing gas at a temperature ranging from 300°-1200° C. to form particles comprising a reducible oxide of antimony, which can be used anew. Parallel methods with different metal oxides are described in U.S. Pat. Nos. 4,443,645 (oxide of germanium); 4,443,646 (oxide of bismuth); 4,443,647 (oxide of lead); 4,443,648 (oxide of indium) and 4,443,649 (oxide of manganese) . However, the yields for C2 + hydrocarbons (as quoted in the examples) are low, reaching a top of 2.1% with a manganese catalyst.
Catalysts comprising supported-Mn using different promoting materials provide an improvement in both selectivity and yield to C2 + hydrocarbons when the above-mentioned cyclic operation is employed (U.S. Pat. Nos. 4,495,374; 4,499,322; 4,547,611; 4,650,781; 4,654,459; 4,777,313, and 4,939,310).
If a solid with an analogous composition is implemented in a co-fed operation, the performance of the process decreases substantially (U.S. Pat. Nos. 4,523,049 and 4,981,829).
Further improvement was proposed by U.S. Pat. No. 4,608,449 when disclosing oxidative coupling of methane by co-feeding methane and oxygen in a reactor at temperatures of 500°-900° C., with molar ratios CH4 /O2 higher than 2 and an overall pressure higher than 1 bar. It is also disclosed that propane is the higher hydrocarbon among C2 + with an overall selectivity to C2 + hydrocarbons (ethane, ethylene and propane) no higher than 65%, and that unreacted methane can be recirculated into the reactor. The catalysts used are metal oxides of B elements of Periodic Table, including lead, bismuth, indium, cadmium, antimony, tin and thalium, either massive or supported on alumina, silica, titania and silicon carbide, which operate in temperature ranges of 500°-900° C. Under these rather severe conditions a part of the metal (i.e. tin) oxide is lost by vaporization, particularly for long periods on-stream. To overcome this inconvenience, U.S. Pat. No. 4,780,449 discloses much more stable catalytic systems for OCM reaction including alkaline-earth and lanthanides, which can be used either alone or with promoters such as alkaline, alkaline-earth and lanthanide oxides up to 50% by weight.
Also, incorporation of halogens to the catalysts (U.S. Pat. No. 4,914,252) or feeding with halogenated hydrocarbons has been described. Halocompounds have the property of generating halogen radicals at high temperatures, which then act as initiators of methyl radicals from methane molecules. Whichever the method, halogen is consumed during OCM reaction with the subsequent production of the corresponding haloacid, which implies serious corrosion problems and requires careful control of the analytical system.
Therefore, it might be concluded that there is no general principle to predict the catalytic behaviour of a given system. Researchers on the art often refer to physical phenomena, such as adsorption-desorption of oxygen species from the catalyst surface or mass, or generation of free radicals, etc. Consequently, the solid materials used in the processes are usually called activators, promoters or catalysts. In this description, the term catalyst will be employed.
Finally, as the dimerization reaction is extremely complex, the adequacy of a given catalyst is unpredictable. It must be also kept in mind that both methane conversion and selectivity to a given product depend on the reaction conditions and mode of operating the reaction, and there is little basis for predicting what operation conditions will result in high conversion yields to a given product, i.e. ethylene and ethane.
It is an object of the invention to provide an improved method for the conversion of methane into longer chain hydrocarbons, with a high selectivity, particularly to ethylene and ethane.
Another object is to provide an OCM method which can be carried out with low cost starting materials and under rather moderate reaction conditions.
It is also an object of the present invention to provide an improved catalyst composition for carrying out the OCM reaction.
According to the invention, methane can be converted into longer chain hydrocarbons, particularly ethylene and ethane, by following a method wherein a methane and oxygen mixture is contacted with a solid catalyst comprising manganese, silicon or aluminum, and alkaline element and a non-metallic element.
The reaction is carried out at atmospheric pressure in a fixed bed flow reactor which operates under the appropriate conditions leading to OCM reaction. The alkaline element is preferably potassium, and the non-metallic element is preferably phosphorus.
Also preferably, the catalyst comprises manganese, silicon, potassium and phosphorus in a molar ratio 0-0.5:93.2-93.7:4.2:2.1, respectively.
The method of the invention is also distinguished from known processes in that the reactant mixture is fed into a fixed bed reactor without diluent; the reaction temperature is kept within a relatively low range of temperature, 600°-850° C.; the catalyst is prepared by combining the precursor materials, calcining in air atmosphere, and preheating within the reactor in the reactant gas mixture before starting catalytic action; manganese and the alkaline element are incorporated simultaneously to the catalyst, and aluminum or silicon are incorporated as oxides during the preparation of the catalyst. All these features lead to large C2 + yields and lower cost of operation.
FIGS. 1 and 2 are ternary diagrams showing the composition of examples of catalysts according to the invention.
The gas fed is methane, although a mixture with non interfering gases can be used if the methane content is within 25-100% molar. Other alternatives to natural gas, as synthetic natural gas (SNG) and products resulting from gasification of carbide materials or from anaerobic digestion of biomass can be also used. The presence of minor amounts of longer chain hydrocarbons in the above feeds does not require further purifications.
The preferred catalysts of the invention for the OCM reaction are mixtures of manganese oxide-silicon oxide or manganese oxide-aluminum oxide, promoted with variable amounts of alkaline metals, preferable potassium, and non-metals, preferably phosphorus.
The amounts of manganese range from 0-8% molar, preferably between 0-1% molar. The alkaline element, potassium, ranges from 0-40% molar, preferably 3-6% molar. The phosphorus content ranges from 0-15% molar, preferably 1.5-3% molar. The balance up to 100% molar is silicon or aluminum.
The composition of the different catalysts is expressed as the molar percentage of manganese, potassium and silicon or aluminum, as represented in the ternary diagrams of FIGS. 1 and 2. It should be noted that only the manganese-potassium-silicon series contains phosphorus, and that the molar ratio phosphorus/potassium was 1:2. For simplicity, two highly loaded potassium catalyst preparations (approx. 36% molar) have not been included in this latter series.
The preferred catalyst results from the combination Mn--Si--K--P, with a molar ratio of 0-0.5:93.2-93.7:4.2:2.1, respectively. The catalyst can be prepared by complete solubilization of alkaline (potassium), phosphorus and manganese precursors. After that, the solubilized materials are contacted with the corresponding silicon or aluminum compound. The resulting mixture is firstly pre-heated to remove volatile elements and then heated at temperatures ranging from 600°-1000° C., preferably 700°-850° C. Moreover, physical shape of the catalyst can accordingly be selected with conventional techniques of the art, namely tablets, beads or extrudates. These operations are carried out in an independent synthesis system.
In accordance with the most extended procedure for the oxidative coupling of methane to higher hydrocarbons, particularly ethylene and ethane, the reaction is carried out in a fixed bed flow reactor by co-feeding both methane and oxygen. This mode of operation provides a great flexibility for the control of the operation parameters and of the overall process, and simultaneously reduces the extremely long time of operation required by the cyclic feeding. The temperature required for the oxidative coupling is in the range of 500°-1000° C., although a narrower range of 600°-800° C. is preferred. The reactor operates in all cases at pressures about 1 bar, and only a slight increase is introduced as a consequence of the pressure drop through the catalyst bed and other flow elements of the system. This feature simplifies to a great extent the control of the operation since a very simple feed system and reactor control are required. Another important advantage arising from these conditions is that of reducing the probability of an explosion. The residence times of reactants are in the range of 0.5-50 g.h/mol, the range of 1-30 g.h/mol being preferable.
According to the invention it has been found that an enhanced methane conversion into longer chain hydrocarbons, particularly ethylene and ethane, via OCM reaction, can be achieved by contacting a methane and oxygen mixture on a catalyst comprising manganese, silicon or aluminum, an alkaline element, preferably potassium, and phosphorus, with a preferred Mn/Si(Al)/K/P molar ratio of 0-0.5:93.2-93.7:4.2:2.1, respectively, under reaction conditions leading to an effective oxidative coupling of methane.
The following examples are given to illustrate specific embodiments of the method according to the invention.
The composition of several catalyst samples, expressed as molar percentage of the constituent elements, is shown in Table I. There are two groups of preparations with the same composition, 1 and 2, 5 and 6. Among these, small differences exist with respect to the general preparation procedure described above. While the pH of the solubilization medium of manganese, potassium and phosphorus precursors was adjusted to the acid region for preparations of catalysts 1 and 5, it remained uncontrolled for all the other catalysts.
TABLE I______________________________________MOLAR COMPOSITION (%) OF THE CATALYSTSCATALYST Mn Si A1 K P______________________________________1 0.0 93.7 0.0 4.2 2.12 0.0 93.7 0.0 4.2 2.13 0.2 93.5 0.0 4.2 2.14 0.2 95.3 0.0 3.0 1.55 0.5 93.2 0.0 4.2 2.16 0.5 93.2 0.0 4.2 2.17 0.8 90.5 0.0 5.8 2.98 0.9 99.1 0.0 0.0 0.09 2.6 0.0 95.9 1.5 0.0______________________________________
The data of Table II provides a summary of both reaction conditions and catalyst performance for each sample. It should be noted that two reaction conditions, W/F=20 g.h/mol for a molar ratio CH4 /O2 =4 and W/F=10 g.h/mol for a molar ratio CH4 /O2 =5, were used. For comparative purposes among the two groups, data of catalyst 5 under the two reaction conditions, 5 and 5a, are shown.
TABLE II______________________________________Catalyst sample 1 1 1 2 2 2______________________________________Residence time 20 20 20 20 20 20(g.h/mol)Molar ratio CH4 /O2 4 4 4 4 4 4Pressure (bar) 1 1 1 1 1 1Temperature (°C.) 700 750 800 700 750 800Methane conversion % 14.0 23.4 25.9 11.9 20.8 24.2Selectivity to C2 + % 15.5 39.9 51.0 7.3 32.1 47.5Ethylene yield % 0.80 5.05 8.16 0.26 3.38 7.00Ethane yield % 1.32 3.62 3.67 0.59 2.90 3.47CO yield % 8.54 6.92 4.42 8.47 6.85 4.10CO2 yield % 3.29 7.15 8.25 2.59 7.29 8.63______________________________________Catalyst sample 3 3 3 4 4 4______________________________________Residence time 20 20 20 20 20 20(g.h/mol)Molar ratio CH4/O 2 4 4 4 4 4 4Pressure (bar) 1 1 1 1 1 1Temperature (°C.) 700 750 800 700 750 800Methane conversion % 16.2 18.6 22.1 17.0 19.6 22.2Selectivity to C2 + % 8.3 22.2 37.9 10.8 26.3 37.8Ethylene yield % 0.33 1.68 4.64 0.52 2.32 4.83Ethane yield % 0.98 2.31 3.05 1.27 2.63 2.93CO yield % 5.25 4.92 3.84 6.12 4.95 3.91CO2 yield % 9.59 9.53 9.88 9.05 9.51 9.89______________________________________Catalyst sample 5 5 5 5a 5a 5a______________________________________Residence time 20 20 20 10 10 10(g.h/mol)Molar ratio CH4 /O2 4 4 4 5 5 5Pressure (bar) 1 1 1 1 1 1Temperature (°C.) 700 750 800 700 750 800Methane conversion % 9.9 21.7 25.5 12.5 17.8 18.5Selectivity to C2 + % 17.5 37.9 50.0 23.1 31.3 21.2Ethylene yield % 0.53 4.30 8.00 1.28 3.70 3.45Ethane yield % 1.16 3.28 3.17 1.60 1.87 0.47CO yield % 5.14 8.03 7.55 -- -- --CO2 yield % 3.03 5.47 5.20 -- -- --______________________________________Catalyst sample 6 6 6 7 7 7______________________________________Residence time 20 20 20 10 10 10(g.h/mol)Molar ratio CH4 /O2 4 4 4 5 5 5Pressure (bar) 1 1 1 1 1 1Temperature (°C.) 700 750 800 700 750 800Methane conversion % 16.6 18.5 22.2 13.8 16.9 --Selectivity to C2 + % 7.1 21.0 37.6 10.1 25.5 --Ethylene yield % 0.31 1.57 4.62 -- -- --Ethane yield % 0.86 2.18 3.07 -- -- --CO yield % 5.20 4.23 3.40 -- -- --CO2 yieid % 10.22 10.4 10.45 -- -- --______________________________________Catalyst sample 8 8 8 9 9 9______________________________________Residence time 10 10 10 10 10 10(q.h/mol)Molar ratio CH4 /O2 5 5 5 5 5 5Pressure (bar) 1 1 1 1 1 1Temperature (°C.) 700 750 800 700 750 800Methane conversion % 14.9 14.6 -- 12.6 14.5 18.3Selectivity to C2 + % 4.7 17.6 -- 9.8 22.9 21.6Ethylene yield % -- -- -- 0.40 2.20 3.44Ethane yield % -- -- -- 0.83 1.13 0.51CO yield % -- -- -- -- -- --CO2 yield % -- -- -- -- -- --______________________________________
|Cited Patent||Filing date||Publication date||Applicant||Title|
|US4495374 *||Aug 12, 1983||Jan 22, 1985||Atlantic Richfield Company||Methane conversion|
|US4499322 *||Aug 12, 1983||Feb 12, 1985||Atlantic Richfield Company||Methane conversion|
|US4523049 *||Apr 16, 1984||Jun 11, 1985||Atlantic Richfield Company||Methane conversion process|
|US4547611 *||Apr 16, 1984||Oct 15, 1985||Atlantic Richfield Company||Methane conversion|
|US4650781 *||Dec 18, 1984||Mar 17, 1987||Atlantic Richfield Company||Alkali promoted manganese oxide compositions containing zirconium|
|US4654459 *||Jan 2, 1986||Mar 31, 1987||Atlantic Richfield Company||Alkali promoted manganese oxide compositions containing barium carbonate|
|US4777313 *||Jun 23, 1986||Oct 11, 1988||Atlantic Richfield Company||Boron-promoted reducible metal oxides and methods of their use|
|US4939310 *||Oct 11, 1988||Jul 3, 1990||The British Petroleum Company P.L.C.||Conversion of methane to higher hydrocarbons|
|US4981829 *||Jun 15, 1989||Jan 1, 1991||Johnson Matthey Public Limited Company||Oxidative conversion of methane to ethylene and ethane|
|US5160502 *||Dec 22, 1986||Nov 3, 1992||Phillips Petroleum Company||Composition of matter and method of oxidative conversion of organic compounds therewith|
|Citing Patent||Filing date||Publication date||Applicant||Title|
|US6793699||Sep 4, 2002||Sep 21, 2004||Dennis D. Coleman||Continuous tracer generation apparatus|
|US7066972 *||Jun 2, 2004||Jun 27, 2006||Coleman Dennis D||Continuous tracer generation apparatus|
|US7223602||Sep 4, 2002||May 29, 2007||Coleman Dennis D||Continuous tracer generation method|
|US7674941||Jun 13, 2008||Mar 9, 2010||Marathon Gtf Technology, Ltd.||Processes for converting gaseous alkanes to liquid hydrocarbons|
|US7838708||Jan 25, 2010||Nov 23, 2010||Grt, Inc.||Hydrocarbon conversion process improvements|
|US7847139||Jul 2, 2008||Dec 7, 2010||Grt, Inc.||Hydrocarbon synthesis|
|US7880041||Feb 1, 2011||Marathon Gtf Technology, Ltd.||Process for converting gaseous alkanes to liquid hydrocarbons|
|US7883568||Feb 5, 2007||Feb 8, 2011||Grt, Inc.||Separation of light gases from halogens|
|US7902113||Mar 8, 2011||Research Institute Of Petroleum Industry (Ripi)||Catalyst direct conversion of methane to ethane and ethylene|
|US7964764||Jan 7, 2010||Jun 21, 2011||Grt, Inc.||Hydrocarbon synthesis|
|US7998438||May 27, 2008||Aug 16, 2011||Grt, Inc.||Zone reactor incorporating reversible hydrogen halide capture and release|
|US8008535||Apr 30, 2008||Aug 30, 2011||Marathon Gtf Technology, Ltd.||Process for converting gaseous alkanes to olefins and liquid hydrocarbons|
|US8053616||Jul 1, 2009||Nov 8, 2011||Grt, Inc.||Continuous process for converting natural gas to liquid hydrocarbons|
|US8173851||Jun 3, 2009||May 8, 2012||Marathon Gtf Technology, Ltd.||Processes for converting gaseous alkanes to liquid hydrocarbons|
|US8198495||Mar 2, 2010||Jun 12, 2012||Marathon Gtf Technology, Ltd.||Processes and systems for the staged synthesis of alkyl bromides|
|US8232441||Jul 13, 2009||Jul 31, 2012||Marathon Gtf Technology, Ltd.||Process for converting gaseous alkanes to liquid hydrocarbons|
|US8273929||Jul 17, 2009||Sep 25, 2012||Grt, Inc.||Continuous process for converting natural gas to liquid hydrocarbons|
|US8282810||Jun 3, 2009||Oct 9, 2012||Marathon Gtf Technology, Ltd.||Bromine-based method and system for converting gaseous alkanes to liquid hydrocarbons using electrolysis for bromine recovery|
|US8367884||Feb 5, 2013||Marathon Gtf Technology, Ltd.||Processes and systems for the staged synthesis of alkyl bromides|
|US8415512||Oct 13, 2010||Apr 9, 2013||Grt, Inc.||Hydrocarbon conversion process improvements|
|US8415517||Jul 17, 2009||Apr 9, 2013||Grt, Inc.||Continuous process for converting natural gas to liquid hydrocarbons|
|US8436220||Jun 10, 2011||May 7, 2013||Marathon Gtf Technology, Ltd.||Processes and systems for demethanization of brominated hydrocarbons|
|US8642822||May 27, 2011||Feb 4, 2014||Marathon Gtf Technology, Ltd.||Processes for converting gaseous alkanes to liquid hydrocarbons using microchannel reactor|
|US8802908||Oct 8, 2012||Aug 12, 2014||Marathon Gtf Technology, Ltd.||Processes and systems for separate, parallel methane and higher alkanes' bromination|
|US8815050||Mar 22, 2011||Aug 26, 2014||Marathon Gtf Technology, Ltd.||Processes and systems for drying liquid bromine|
|US8829256||Jun 30, 2011||Sep 9, 2014||Gtc Technology Us, Llc||Processes and systems for fractionation of brominated hydrocarbons in the conversion of natural gas to liquid hydrocarbons|
|US8921256||May 24, 2012||Dec 30, 2014||Siluria Technologies, Inc.||Catalysts for petrochemical catalysis|
|US8921625||Jul 17, 2009||Dec 30, 2014||Reaction35, LLC||Continuous process for converting natural gas to liquid hydrocarbons|
|US8962517||Nov 29, 2012||Feb 24, 2015||Siluria Technologies, Inc.||Nanowire catalysts and methods for their use and preparation|
|US9040762||Oct 17, 2014||May 26, 2015||Siluria Technologies, Inc.||Catalysts for petrochemical catalysis|
|US9133078||Dec 13, 2012||Sep 15, 2015||Gtc Technology Us, Llc||Processes and systems for the staged synthesis of alkyl bromides|
|US9133079||Jan 11, 2013||Sep 15, 2015||Siluria Technologies, Inc.||Process for separating hydrocarbon compounds|
|US9193641||Dec 4, 2012||Nov 24, 2015||Gtc Technology Us, Llc||Processes and systems for conversion of alkyl bromides to higher molecular weight hydrocarbons in circulating catalyst reactor-regenerator systems|
|US9206093||Apr 17, 2014||Dec 8, 2015||Gtc Technology Us, Llc||Process for converting gaseous alkanes to liquid hydrocarbons|
|US20040033167 *||Sep 4, 2002||Feb 19, 2004||Coleman Dennis D.||Continuous tracer generation apparatus|
|US20040072355 *||Sep 4, 2002||Apr 15, 2004||Coleman Dennis D.||Continuous tracer generation method|
|US20050045467 *||Sep 3, 2003||Mar 3, 2005||King Fahd University Of Petroleum And Minerals||Method for the conversion of methane into hydrogen and higher hydrocarbons using UV laser|
|US20050056082 *||Jun 2, 2004||Mar 17, 2005||Coleman Dennis D.||Continuous tracer generation apparatus|
|US20060155157 *||Sep 6, 2005||Jul 13, 2006||Saeed Zarrinpashne||Catalyst direct conversion of methane to ethane and ethylene|
|CN1325164C *||Aug 20, 2004||Jul 11, 2007||东南大学||Manganese series methane oxidation coupling catalyst using multicomponent promoter and its preparation method|
|U.S. Classification||585/500, 585/417, 585/656, 585/943, 585/654, 585/415, 585/658, 585/418|
|Cooperative Classification||Y10S585/943, C07C2/84, C07C2523/04, C07C2523/34, C07C2521/08, C07C2527/18|
|Aug 4, 1997||AS||Assignment|
Owner name: REPSOL PETROLEO S.A., SPAIN
Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNOR:REPSOL, S.A.;REEL/FRAME:008638/0645
Effective date: 19970702
|Apr 5, 2002||FPAY||Fee payment|
Year of fee payment: 4
|Apr 26, 2006||REMI||Maintenance fee reminder mailed|
|Oct 6, 2006||LAPS||Lapse for failure to pay maintenance fees|
|Dec 5, 2006||FP||Expired due to failure to pay maintenance fee|
Effective date: 20061006